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EP3059005B1 - Separation d'un catalyseur homogene d'un melange reactif a l'aide d'une nanofiltration organophilique en tenant compte notamment d'un indicateur de performance a membrane - Google Patents

Separation d'un catalyseur homogene d'un melange reactif a l'aide d'une nanofiltration organophilique en tenant compte notamment d'un indicateur de performance a membrane Download PDF

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EP3059005B1
EP3059005B1 EP16155014.0A EP16155014A EP3059005B1 EP 3059005 B1 EP3059005 B1 EP 3059005B1 EP 16155014 A EP16155014 A EP 16155014A EP 3059005 B1 EP3059005 B1 EP 3059005B1
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membrane
mpi
metal
catalyst
homogeneous catalyst
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EP3059005A1 (fr
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Frank GEILEN
Robert Franke
Bart Hamers
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Evonik Operations GmbH
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Evonik Degussa GmbH
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/027—Nanofiltration
    • B—PERFORMING OPERATIONS; TRANSPORTING
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    • B01J31/40—Regeneration or reactivation
    • B01J31/4015—Regeneration or reactivation of catalysts containing metals
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    • B01D71/00—Semi-permeable membranes for separation processes or apparatus characterised by the material; Manufacturing processes specially adapted therefor
    • B01D71/06—Organic material
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    • B01J31/16—Catalysts comprising hydrides, coordination complexes or organic compounds containing coordination complexes
    • B01J31/18—Catalysts comprising hydrides, coordination complexes or organic compounds containing coordination complexes containing nitrogen, phosphorus, arsenic or antimony as complexing atoms, e.g. in pyridine ligands, or in resonance therewith, e.g. in isocyanide ligands C=N-R or as complexed central atoms
    • B01J31/1845—Catalysts comprising hydrides, coordination complexes or organic compounds containing coordination complexes containing nitrogen, phosphorus, arsenic or antimony as complexing atoms, e.g. in pyridine ligands, or in resonance therewith, e.g. in isocyanide ligands C=N-R or as complexed central atoms the ligands containing phosphorus
    • B01J31/185—Phosphites ((RO)3P), their isomeric phosphonates (R(RO)2P=O) and RO-substitution derivatives thereof
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    • B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
    • B01J31/16—Catalysts comprising hydrides, coordination complexes or organic compounds containing coordination complexes
    • B01J31/24—Phosphines, i.e. phosphorus bonded to only carbon atoms, or to both carbon and hydrogen atoms, including e.g. sp2-hybridised phosphorus compounds such as phosphabenzene, phosphole or anionic phospholide ligands
    • B01J31/2404—Cyclic ligands, including e.g. non-condensed polycyclic ligands, the phosphine-P atom being a ring member or a substituent on the ring
    • B01J31/2409—Cyclic ligands, including e.g. non-condensed polycyclic ligands, the phosphine-P atom being a ring member or a substituent on the ring with more than one complexing phosphine-P atom
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    • B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
    • B01J31/40—Regeneration or reactivation
    • B01J31/4015—Regeneration or reactivation of catalysts containing metals
    • B01J31/4023—Regeneration or reactivation of catalysts containing metals containing iron group metals, noble metals or copper
    • B01J31/4038—Regeneration or reactivation of catalysts containing metals containing iron group metals, noble metals or copper containing noble metals
    • B01J31/4046—Regeneration or reactivation of catalysts containing metals containing iron group metals, noble metals or copper containing noble metals containing rhodium
    • B—PERFORMING OPERATIONS; TRANSPORTING
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    • B01D2311/25—Recirculation, recycling or bypass, e.g. recirculation of concentrate into the feed
    • B01D2311/252—Recirculation of concentrate
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2313/00—Details relating to membrane modules or apparatus
    • B01D2313/70—Control means using a programmable logic controller [PLC] or a computer
    • B01D2313/701—Control means using a programmable logic controller [PLC] or a computer comprising a software program or a logic diagram
    • B—PERFORMING OPERATIONS; TRANSPORTING
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    • B01J2231/30—Addition reactions at carbon centres, i.e. to either C-C or C-X multiple bonds
    • B01J2231/32—Addition reactions to C=C or C-C triple bonds
    • B01J2231/321—Hydroformylation, metalformylation, carbonylation or hydroaminomethylation
    • B—PERFORMING OPERATIONS; TRANSPORTING
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    • B01J2231/00—Catalytic reactions performed with catalysts classified in B01J31/00
    • B01J2231/60—Reduction reactions, e.g. hydrogenation
    • B01J2231/64—Reductions in general of organic substrates, e.g. hydride reductions or hydrogenations
    • B01J2231/641—Hydrogenation of organic substrates, i.e. H2 or H-transfer hydrogenations, e.g. Fischer-Tropsch processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01J2231/00—Catalytic reactions performed with catalysts classified in B01J31/00
    • B01J2231/60—Reduction reactions, e.g. hydrogenation
    • B01J2231/64—Reductions in general of organic substrates, e.g. hydride reductions or hydrogenations
    • B01J2231/641—Hydrogenation of organic substrates, i.e. H2 or H-transfer hydrogenations, e.g. Fischer-Tropsch processes
    • B01J2231/643—Hydrogenation of organic substrates, i.e. H2 or H-transfer hydrogenations, e.g. Fischer-Tropsch processes of R2C=O or R2C=NR (R= C, H)
    • B—PERFORMING OPERATIONS; TRANSPORTING
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    • B01J2531/00—Additional information regarding catalytic systems classified in B01J31/00
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    • B01J2531/18—Gold
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    • B01J2531/80—Complexes comprising metals of Group VIII as the central metal
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    • B01J2531/822—Rhodium

Definitions

  • the retention can thus assume values from 0 to 1 and is therefore given in%.
  • a retention of 0% means that the considered component permeates just as well as the solvent, so that the Mass fractions of the components in the retentate are the same as in the permeate.
  • Permeability P and retention R are given by the separating active material of the membrane as well as by the composition of the substance mixture to be separated. When designing a membrane separation process, these parameters are always considerable. Due to the substance dependence of these parameters, they are determined by the choice of membrane material. Therefore, selection of the separating active membrane material for the respective separation task is decisive for the entire process design.
  • Catalysts are used to accelerate chemical reactions without being self-consumed. In industrial chemistry, catalysts make the realization of reactions economical or even possible. That is why catalysts are of great value in the chemical industry. Since the catalysts are not consumed, they can be separated and recycled after completion of the reaction catalyzed by them. Of the Effort which must be operated or operated for catalyst removal depends on the value and the type of catalyst.
  • the catalyst used in the hydroformylation include organometallic complex compounds which have a metal as the central atom which is complexed with various ligands. Frequently used as ligands organophosphorus compounds, non-limiting examples are organophosphines, organophosphites or Organophosphoramidite. Such a catalyst system is dissolved in the liquid reaction mixture of olefin and synthesis gas dissolved therein and is thus homogeneous.
  • This example describes the procedure for determining the membrane performance indicator MPI.
  • the membrane to be tested is examined in a crossflow filtration experiment.
  • the basic apparatus design for these experiments is in FIG. 3 shown.
  • the mass concentration (or the mass fraction) of the component to be retained (represented by the central atom in the catalyst complex) in the retentate stream w R and in the permeate stream w P must be analyzed.
  • samples can be taken from the plant by techniques known to those skilled in the art and a suitable analysis can be supplied.
  • the stirred tank 2 was the in FIG. 3 shown plant filled with a mixture which corresponds to a derived from a hydroformylation reaction mixture.
  • a mixture hereinafter called INAL, having the composition: isononanal > 85% by weight isononanol ⁇ 3% by weight Di-n-butene ⁇ 5% by weight C8-alkanes ⁇ 1% by weight high boiling ⁇ 10% by weight as much (acetylacetonato) dicarbonylrhodium (I) (eg CARAC, the company Umicore or Heraeus) and tris (2,4-di-tert-butylphenyl) phosphite (eg Alkanox 240 from Addivant) given that a rhodium content of 75 to Adjusted 90 mg / kg mixture.
  • I acetylacetonato dicarbonylrhodium
  • tris (2,4-di-tert-butylphenyl) phosphite
  • Rh support permeability MPI [%] [kg / (m2h bar)] Rh @ 25 EUR / g Rh @ 50 EUR / g Rh @ 75 EUR / g Rh @ 100 EUR / g A 93.8 0.86 12:35 12:30 12:30 12:25 B 98.5 0.30 12:15 12:20 12:20 12:20 C 97.4 0.40 12:25 12:25 12:25 D 90.0 0.30 12:05 00:00 00:00 00:00 e 74.7 2.66 12:25 12:10 12:05 00:00 F 97.3 0.50 12:30 12:30 12:30 12:30 12:30 G 93.9 1.13 12:40 12:40 12:40 12:35 H 94.4 0.95 12:40 12:35 12:35 12:35 I 89.6 1.49 12:35 12:30 12:25 12:20 J 95.1 0.83 12:35 12:35 12:35 12:35 K 91.1 1.55 12:40 12:35 12:35 12:30 L 94.0 1.32 12:45 12:45 12:45 12:45 M
  • the core of the plant is a hydroformylation reactor 1.
  • the hydroformylation reaction takes place.
  • an olefin 2 is reacted with synthesis gas 3 - a mixture of carbon monoxide and hydrogen - in the presence of a homogeneously dissolved catalyst to give corresponding aldehydes having one more carbon atom.
  • This reaction is a gas / liquid phase reaction in which the olefin and the reaction products are in the liquid phase, while a portion of the synthesis gas 3 forms the gas phase and another part of the synthesis gas is dissolved in the liquid phase. Also dissolved in the liquid phase is a homogeneous catalyst complex.
  • a first heat exchanger 5 the hydroformylation discharge 4 is cooled to a temperature of about 40 to 50 ° C.
  • a first degasser 9a the hydroformylation discharge 4 is depressurized to about 0.5 MPa and the synthesis gas 3 bubbling back into the reactor 1 is recycled. Then, the hydroformylation discharge 4 of a first membrane separation unit 6 is abandoned.
  • the membrane separation unit 6 is a multi-stage output cascade, as known from the prior art (eg DE102013203117 A1 However, it is sufficient for the functional relationship to regard the first membrane separation unit 6 as a single membrane.
  • membranes which comprise a release-active layer of a material selected from cellulose acetate, cellulose triacetate, cellulose nitrate, regenerated cellulose, polyimides, polyamides, polyether ether ketones, sulfonated polyether ether ketones, aromatic polyamides, polyamidimides, polybenzimidazoles, polybenzimidazolones, polyacrylonitrile, polyaryl ether sulfones, polyesters, polycarbonates, Polytetrafluoroethylene, polyvinylidene fluoride, polypropylene, siloxane terminally or organically modified siloxane, polydimethylsiloxane, silicones, polyphosphazenes, polyphenylsulfides, polybenzimidazoles, 6.6 nylon®, polysulfones, polyanilines, polypropylenes, polyurethanes, acrylonitrile / glycidyl methacrylate (PANGMA), polytri
  • the product stream 7 is evaporated under the action of heat.
  • a bottom temperature of 90 ° C is set on the falling film evaporator; the bottom temperature at the thin film evaporator is 100 ° C.
  • the evaporation is assisted by an applied vacuum of about 30 hPa in each case. In this way, more than 90% of the mass introduced into the thermal separation unit 10 with the product stream 7 evaporates. This vaporous mass forms the top product 11 of the thermal separation unit. Since the components introduced have different boiling points, evaporation not only results in a purely quantitative separation of the product stream 7 but also in a qualitative manner.
  • the function of the adsorber 13 is to Residual amounts of catalyst, in particular noble metal, which was entrained in droplets with the steam to catch. This is achieved by using a conventional adsorbent such as activated carbon, silicates or aluminum oxides, which are used as a fixed bed. The adsorption is carried out at a temperature between 30 and 140 ° C and space loads of 0.01 to 5 1 / h.
  • catalyst in particular noble metal
  • the hydrogenation can also be arranged after the thermal workup, once for the alcohol-rich fraction 17 (which is rather rich in aldehydes in this case) and once for the high boiler fraction 19.
  • the low boiler fraction 18 then contains the unreacted alkenes and can be recycled to the hydroformylation reactor 1 (not shown in this figure).
  • the top product 11 is thus not completely, but only partially fed to the hydrogenation at a Alkkengurment, the alkenes are previously separated and recycled.
  • the bottom product 12 of the thermal separation unit 10 essentially contains the high boilers, smaller amounts of aldehyde and catalyst.
  • the mass flow of the bottom product 12 is significantly smaller than that of the overhead product. If the product flow is 30 tons per hour and the proviso that 90% of the incorporated mass leaves the thermal separation unit 10 overhead, the mass flow of the bottom product 12 is only 3 t per hour, ie 1/9 of the overhead product.
  • the largely consisting of high boilers and residual aldehyde permeate 21 of the second membrane separation unit 20 is passed through a second adsorber 24 to receive and secure residual amounts of catalyst.
  • the adsorption is carried out at a temperature of 30 to 140 ° C and space loads of 0.01 to 5 1 / h.
  • the adsorbent is used as a fixed bed.
  • Example 4 selected membranes from Example 1 are used in a reaction system comprising isononanol (desired product), isononanal (intermediate), high-boiling by-products, and a homogeneous hydrogenation catalyst.
  • the hydrogenation catalyst may be present as a defined complex, but more likely is a mixture of different organometallic complex species, as well as their degradation products.
  • the unit is connected in two stages in order to increase the retention, the required membrane area results from the permeability of the membranes and is shown in Table 5.
  • Catalyst-depleted permeate can then be fed to further work-up steps (for example distillation).
  • the ruthenium mass fraction w (Ru) in the permeate is given in Table 5.
  • Catalyst-rich retentate is fed back into the reactor as a catalyst circulation.
  • the proportionate production costs were estimated using the following assumptions: The total ruthenium leaving the plant via the nanofiltration permeate must be re-purchased at market prices. Three assumed market prices were included in the calculation and are shown in Table 5.
  • the membranes all have a market price of 1000 EUR per square meter and a life of 2 years, so that each year half of the required membrane area must be replaced.
  • the initial assembly is one of the investment costs and is not included in the calculation.
  • Table 5 Ru mass fraction, membrane area and pro-rata production costs Bez.
  • Membranes E to P also show that a rating based solely on the retention is not expedient because it is not always the membranes with the highest retention that also have the best (highest) MPI. However, it is immediately apparent from Table 3 that the membranes with a lower MPI generally lead to higher production costs.

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Claims (5)

  1. Procédé de séparation d'un catalyseur homogène ou au moins de constituants ou de produits de décomposition de celui-ci d'un mélange réactionnel à l'aide d'une nanofiltration organophile, selon lequel un mélange réactionnel comprenant un solvant organique liquide et un catalyseur homogène dissous dans celui-ci et/ou des constituants et/ou des produits de décomposition du catalyseur homogène est introduit sur une membrane et y est séparé en un rétentat et en un perméat, le catalyseur homogène ou ses constituants et/ou produits de décomposition s'accumulant dans le rétentat, de telle sorte que la concentration du catalyseur homogène ou de ses constituants et/ou produits de décomposition dans le rétentat soit supérieure à celle dans le perméat et dans le mélange réactionnel, et le catalyseur homogène consistant en un composé complexe métallo-organique comprenant un métal en tant qu'atome central, caractérisé en ce que la séparation est ajustée de telle sorte qu'elle ait lieu à un indicateur de puissance de membrane MPI sans dimension supérieur à 0,35, l'indicateur de puissance de membrane étant défini par : MPI = 0,5 R S / 7 1 + P S / 100 * R − 1 / 10 * P
    Figure imgb0016
     R représentant la rétention de la membrane sans dimension au regard du métal ou au regard des autres constituants et/ou produits de décomposition du catalyseur homogène, et P représentant la perméabilité de la membrane en kg/(m2*bar*h) et S représentant un prix du marché supposé ou le prix du marché actuel du métal ou des autres constituants et/ou produits de décomposition du catalyseur homogène en Euro/g.
  2. Dispositif pour la séparation d'un catalyseur homogène et/ou au moins de constituants et/ou produits de décomposition de celui-ci d'un mélange réactionnel par nanofiltration organophile, comprenant une membrane, qui comprend une entrée pour une alimentation, une sortie pour un rétentat et une sortie pour un perméat, caractérisé en ce que la membrane est dimensionnée de telle sorte qu'un indicateur de puissance de membrane MPI sans dimension en mode normal du dispositif soit d'au moins 0,35, l'indicateur de puissance de membrane étant défini par : MPI = 0,5 R S / 7 1 + P S / 100 * R − 1 / 10 * P
    Figure imgb0017
     R représentant la rétention de la membrane sans dimension au regard du métal ou au regard des autres constituants et/ou produits de décomposition du catalyseur homogène, et P représentant la perméabilité de la membrane en kg/(m2*bar*h) et S représentant un prix du marché supposé ou le prix du marché actuel du métal ou des autres constituants et/ou produits de décomposition du catalyseur homogène en Euro/g, et le catalyseur homogène consistant en un composé complexe métallo-organique comprenant ledit métal en tant qu'atome central, et le dispositif comprenant un réglage qui est conçu pour ajuster au moins un paramètre d'exploitation du dispositif de telle sorte que la valeur réelle de l'indicateur de puissance de membrane du dispositif soit ajustée à une valeur de consigne supérieure ou égale à 0,35 de l'indicateur de puissance de membrane.
  3. Article selon l'une quelconque des revendications 1 à 2, dans lequel le MPI est d'au moins 0,5 ou supérieur à 0,75.
  4. Article selon la revendication 1 ou 2, dans lequel la membrane comprend une couche à action de séparation en acrylate de silicone.
  5. Article selon l'une quelconque des revendications 1 à 4, caractérisé en ce que le mélange réactionnel provient indirectement ou directement d'une réaction chimique qui est choisie dans le groupe comprenant les types de réactions suivants : hydroformylation, hydrocarboxylation, alcoxycarbonylation, méthoxycarbonylation, hydrogénation, hydrocyanation ;
    et en ce que le catalyseur homogène consiste en un composé complexe métallo-organique dont l'atome central est choisi dans le groupe comprenant les métaux suivants : cobalt, rhodium, iridium, ruthénium, palladium ;
    à condition que le catalyseur homogène choisi catalyse la réaction chimique choisie de telle sorte que le mélange réactionnel soit obtenu.
EP16155014.0A 2015-02-18 2016-02-10 Separation d'un catalyseur homogene d'un melange reactif a l'aide d'une nanofiltration organophilique en tenant compte notamment d'un indicateur de performance a membrane Active EP3059005B1 (fr)

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